High efficiency electrolysis cell for generating oxidants in solutions

ABSTRACT

A method for killing microorganisms in water, by passing an aqueous feed solution comprising of water containing some form of halide salt into a non-membrane electrolysis cell comprising an anode and a cathode, adjacent to the anode, while flowing electrical current between the anode and the cathode to electrolyze the aqueous feed solution and convert the halide salt to anti-microbial mixed oxidants.

FIELD OF THE INVENTION

[0001] This invention relates to devices and methods for generatingmixed oxidants, such as hypochlorite and chlorine, from aqueoussolutions containing naturally present salts (e.g. naturally presentNaCl) or added salts (e.g. added NaCl). Our approach employs a voltagepotential across a pair of electrodes to induce current flow through thewater, to electrolyze the water that passes between the electrodes,thereby sterilizing the water. As contaminated water passes between theelectrodes, the microorganisms are killed and the water is sterilized.Additionally, the treated water also retains some residual biocidalbenefit, due to the reactions involving residual chloride ions withinthe water that generate biocidal agents such as free chlorine (Cl₂),hypochlorous acid ions (OCL⁻), and other biocidal ions and freeradicals. Two of the key parameters that have led to the improvements inefficiency of the electrolysis of the chloride ions, to enable effectivekill of microorganisms in water, are the elimination of the membraneseparating the anode and cathode and the close proximity of the twoelectrodes (e.g. <0.5 mm). As a result, we have developed several small,efficient, portable, battery-powered devices that can effectively killmicroorganisms in contaminated solutions.

BACKGROUND OF THE INVENTION

[0002] Various oxidants, such as hypochlorite, chlorine, chlorinedioxide and other chlorine based oxidants, are some of the mosteffective antimicrobial agents for use in industrial and domesticprocess and services, and for commercial and consumer products. Thestrong oxidative potential of these oxidant molecules make it ideal fora wide variety of uses that include disinfecting and sterilizing.Concentrations of oxidant species in an aqueous solution as low as 1part per million (ppm) or less, are known to kill a wide variety ofmicroorganisms, including bacteria, viruses, molds, fungi, and spores.Higher concentrations of oxidants, up to several hundred ppms, provideeven higher disinfection and oxidation of numerous compounds for avariety of applications, including the wastewater treatment, industrialwater treatment (e.g. cooling water), fruit-vegetable disinfection, oilindustry treatment of sulfites, textile industry, and medical wastetreatment. Oxidants can react with and break down phenolic compounds,and thereby removing phenolic-based tastes and odors from water.Oxidants are also used in treating drinking water and wastewater toeliminate cyanides, sulfides, aldehydes and mercaptans.

[0003] While separate-compartment, membrane-containing electrolysiscells have been used to make hypochlorite and other oxidants on acommercial scale, they have not been completely satisfactory at theconsumer level (i.e. small and portable). Even though there have beensome electrochemical units that we developed for consumer applicationsusing the electrochemical approach, these have proven to be moreexpensive to produce and have required larger amounts of power toachieve the desired efficacy. The electrolysis cells in commercial use,and disclosed in the prior art that utilize ion permeable membranes ordiaphragms, require that the anolyte solution be substantially free ofdivalent cations, such as magnesium and calcium, to avoid the formationof precipitated calcium or magnesium salts that would quickly block andcover the membrane, and significantly reduce or stop the electrolysisreaction.

[0004] Consequently, there remains a need for a simple, safe method andapparatus for manufacturing these antimicrobial oxidants for domesticuses, under a wide variety of situations. The present inventiondescribes a method and an apparatus for making antimicrobial oxidantsinexpensively, easily and effectively.

SUMMARY OF THE INVENTION

[0005] The present invention relates to a method for makingantimicrobial oxidants from an aqueous solution comprising of naturallypresent salts (e.g. water naturally containing NaCl), or added salts(e.g. water to which NaCl was added) using a non-membrane electrolysiscell. A non-membrane electrolysis cell is an electrolysis cell thatcomprises an anode electrode and a cathode electrode, and having a cellchamber, and which does not have an ion permeable membrane that dividesthe cell passage into two (or more) distinct anode and cathode chambers.The various salts are converted to antimicrobial oxidants as electricitypasses through the aqueous feed solution in a passage that forms aportion of the cell chamber adjacent to the surface of the anode.

[0006] The present invention provides a method for making antimicrobialoxidants, comprising the steps of: (1) providing an aqueous feedsolution comprising of natural water or water to which a chloride saltis already present or to which chloride salt has been added; (2) passingthe aqueous feed solution into a cell chamber of a non-membraneelectrolysis cell comprising an anode and a cathode, and along a passageadjacent to the anode; (3) flowing an electrical current between theanode and the cathode, thereby electrolyzing the aqueous feed solutionin the passage, whereby a portion of the salt in the passage isconverted to antimicrobial oxidants; and (4) passing the electrolyzedaqueous solution out of the electrolysis cell, thereby forming anaqueous effluent comprising antimicrobial oxidants not needed based onthe approach we chose as listed in claims 1.

BRIEF DESCRIPTION OF THE DRAWINGS

[0007] The various advantages of the present invention will becomeapparent to skilled artisans after studying the following specificationand by reference to the drawings in which:

[0008]FIG. 1 shows an electrolysis cell used in the practice of thepresent invention;

[0009]FIG. 2 shows a sectional view of the electrolysis cell of FIG. 1though line 2-2;

[0010]FIG. 3 shows a sectional view of an alternative electrolysis cellused in the practice of the present invention;

[0011]FIG. 4 is a sectional view of another electrolysis cell having aporous anode;

[0012]FIG. 5 is a sectional view of yet another electrolysis cell havinga porous anode;

[0013]FIG. 6 is a sectional view of another electrolysis cell having aporous anode and a porous flow barrier;

[0014]FIG. 7 is a sectional view of yet another electrolysis cell havinga porous anode and a porous flow barrier;

[0015]FIG. 8 is a sectional view of still another electrolysis cellhaving a porous anode and a porous flow barrier;

[0016]FIG. 9 is a block diagram of a flow cell configuration;

[0017]FIG. 10 is a block diagram of a recirculation cell configuration;

[0018]FIG. 11 is a block diagram of a flow cell having a filtermechanism;

[0019]FIG. 12 is a block diagram of a recirculation cell having a filtermechanism;

[0020]FIG. 13 is a block diagram of a flow cell having an off/on sensor;

[0021]FIG. 14 is a block diagram of a recirculation cell having anoff/on sensor;

[0022]FIG. 15 is a block diagram of a flow cell having an ion exchangeresin; and

[0023]FIG. 16 is a block diagram of a recirculation cell having an ionexchange resin.

DETAILED DESCRIPTION OF THE INVENTION

[0024] The present invention employs an electrical current passingthrough an aqueous feed solution between an anode and a cathode toconvert low levels of salt precursors, whether they are naturallypresent in water (e.g. rivers or wells) or later dissolved within thesolution (e.g. added salts such as NaCl). When an aqueous solution flowsthrough the chamber of the electrolysis cell, and electrical current ispassed between the anode and the cathode, several chemical reactionsoccur that involve the water, as well as one or more of the other saltsor ions contained in the aqueous solution.

[0025] At the anode, within a narrow layer of the aqueous solution inthe passage adjacent to the anode surface, the following chlorinegenerating reaction occurs:

2Cl⁻←→Cl₂ (g)+2e⁻.

[0026] Chlorine gas (Cl₂) generated by the chlorine reaction dissolvesin the water to generate hypochlorite ions (OCL⁻). Note that severalother potential chlorine-oxygen reactions (e.g. chlorine dioxide) mayalso take place. Without being bound by any particular theory, it isbelieved that the anode electrode withdraws electrons from the water andother ions adjacent to the anode, which results in the formation ofantimicrobial oxidative species in the narrow surface layer of aqueousfeed solution. This surface layer, at the anode interface, is believedto be about 100 nanometers in thickness. As a result, the smaller gapsize has led to higher efficiency conversion than a larger gap size. Ofcourse, a certain limitation will exist as which point it is no longerpossible to flow the aqueous solution without significant back pressureor the gap is so small that a very large current is drawn due to the lowresistance between the electrodes. Flow dynamics, which include themovement of molecules in a flowing solution by turbulence, predict thatthe conversion of salts will increase as the solution flow path nearsthe anode surface layer. Consequently, electrolysis cells andelectrolysis systems of the present invention preferably maximize theflow of the aqueous feed solution through this surface layer adjacentthe anode, in order to maximize the conversion of antimicrobialoxidants. Additionally, the removal of the membrane, that typicallyseparates the anode and cathode compartment, also increases the reactionrate by preventing the slow migration of ions across this membrane.

[0027] The present invention relates to the production of one or moremixed oxidant products and can include hypochlorite, chlorine, chlorinedioxide, ozone, hydrogen peroxide, and several other chlor-oxigenatedspecies.

[0028] The aqueous feed solution comprises of an electrolytic solutionmade of at least one halide salt, which for simplicity will beexemplified herein after by the most preferred halide salt, sodiumchloride. Sodium chloride is a salt ordinarily found in tap water, wellwater, and other water sources. Consequently, there is usuallysufficient chloride ion in the water to yield a desired concentration ofmixed oxidants. It is also possible that an amount of the sodiumchloride salt is added into the aqueous feed solution at a desiredconcentration generally of at least 0.1 ppm.

[0029] The level of chloride salt comprised in the aqueous feed solutioncan be selected based on the level of disinfection required by thechlorine containing species (e.g. hypochlorite), in addition to theconversion efficiency of the electrolysis cell to convert the sodiumchloride to the mixed oxidant products. The level of sodium chloridenaturally present or added is generally from about 1 ppm to about 500ppm. For disinfection of a water source, a sodium chloride level ispreferably from about 1 ppm to about 300 ppm, and more preferably about10 ppm to about 200 ppm. The resulting mixed oxidant product level isfrom about 0.1 ppm to about 10 ppm, preferably from about 1 ppm to about2 ppm

[0030] The range of mixed oxidant conversion from the chloride salt thatis achievable in the electrolysis cells of the present inventiongenerally ranges from less than about 1% to about 99%. The level ofconversion is dependent most significantly on the design of theelectrolysis cell, herein after described, as well as on the electricalcurrent properties used in the electrolysis cell.

[0031] The aqueous feed solution can optionally comprise one or moreother salts in addition to the sodium chloride. These optional salts canbe used to enhance the disinfection performance of the effluent that isdischarged from the electrolysis cell, or to provide other mixedoxidants in response to the passing of electrical current through theelectrolysis cell. Another preferred salt is sodium bromide. A preferredapparatus and method for electrolyzing aqueous solutions comprisingalkali halides is disclosed in co-pending, commonly assigned U.S.provisional patent application 60/280,913 (Docket 8492P), filed on Apr.2, 2001. Other preferred salts consist of alkali halite, and mostpreferably sodium chlorite. A preferred apparatus and method forelectrolyzing aqueous solutions comprising alkali halites is disclosedin as exampled in U.S. patent application Ser. No. 09/947,846 which ishereby incorporated by reference.

[0032] The present invention can optionally use a local source ofchloride salt, and a means for delivering the chloride salt to theaqueous feed solution. This embodiment is advantageously used in thosesituations when the target water to be treated with the electrolysiscell does not contain a sufficient amount, or any, of the chloride salt.The local source of chloride salt can be released into a stream of theaqueous solution, which then passes through the electrolysis cell. Thelocal source of chloride salt can also be released into a portion of areservoir of aqueous solution, which portion is then drawn into theelectrolysis cell. Preferably, all the local source of chloride saltpasses through the electrolysis cell, to maximize the conversion tomixed oxidants, and to limit the addition of salts to the reservoirgenerally. The local source of chloride salt can also supplement anyresidual levels of chloride salt already contained in the aqueoussolution.

[0033] The local source of chloride salt can be a concentrated brinesolution, a salt tablet in fluid contact with the reservoir ofelectrolytic solution, or both. A preferred local source of chloridesalt is a solid or powdered material. The means for delivering the localsource of chloride salt can comprise a salt chamber comprising thechloride salt, preferably a pill or tablet, through which a portion ofthe aqueous solution passes, thereby dissolving a portion of thechloride salt to form the aqueous feed solution. The salt chamber cancomprise a salt void formed in the body of the device that holds theelectrolysis cell, which is positioned in fluid communication with theportion of aqueous solution that will pass through the electrolysiscell.

[0034] Any water source can be used to form the aqueous feed solution,including well water, tap water, softened water, and industrial processwater, and waste waters. However, for many applications of theinvention, untreated water, such as river water or well water is mostpreferred to form an effluent solution with essentially only naturallypresent chloride ions present. Since these types of natural watercontain sufficient amounts of salts, including sodium chloride,appreciable amounts of mixed oxidants will be formed.

[0035] The addition of other salts or electrolytes into the selectedwater source will increase the conductivity of the water, which willincrease the amount of mixed oxidants produced. However, the increase inconductivity may not result in higher productivity efficiency, since theincrease in conductivity will increase the current draw. Therefore,while more mixed oxidants will be produced, more power will be drawn. Asuitable mixed oxidant productivity equation is expressed by equation I,

η=(CMO*Q)/(I*V)  (I)

[0036] wherein:

[0037] η units are micrograms of mixed oxidant per minute, per watt ofpower used;

[0038] CMO is the concentration of the generated mixed oxidants inmilligrams per liter (mg/l);

[0039] I is the electric current in amps;

[0040] Q is the volumetric flow rate in milliliters per minute (ml/m);and

[0041] V is electric potential across the cell in volts.

[0042] The aqueous feed solution containing the sodium chloride can befed to the electrolysis cell from a batch storage container.Alternatively, the feed solution can be prepared continuously byadmixing a concentrated aqueous solution of sodium chloride with asecond water source, and passing continuously the admixture to theelectrolysis cell. Optionally, a portion of the aqueous feed solutioncan comprise a recycled portion of the effluent from the electrolysiscell. And, the aqueous feed solution can comprise a combination of anyof the forgoing sources. The aqueous feed solution can flow continuouslyor periodically through the electrolysis cell.

Electrolysis Cell

[0043] The electrolysis cell generates mixed oxidants from the chlorideions by flowing electrical current through the aqueous feed solutionthat passes through the cell chamber. The non-barrier electrolytic cellcomprises at least a pair of electrodes, an anode and a cathode. Thecell also comprises a cell chamber through which the aqueous feedsolution passes, and includes a passage that is adjacent to the anode.The passage includes the narrow surface layer adjacent to the anodesurface where the conversion reaction occurs. It is preferred to pass asmuch of the mass of the aqueous effluent solution through the passageand its narrow anode surface region as possible.

[0044] In one embodiment of the present invention, the cell comprises ananode and a confronting (and preferably, co-extensive) cathode that areseparated by a cell chamber that has a shape defined by the confrontingsurfaces of the pair of electrodes. The cell chamber has a cell gap,which is the perpendicular distance between the two confrontingelectrodes. Typically, the cell gap will be substantially constantacross the confronting surfaces of the electrodes. The cell gap ispreferably 0.5 mm or less, more preferably 0.2 mm or less.

[0045] The electrolysis cell can also comprise two or more anodes, ortwo or more cathodes. The anode and cathode plates are alternated sothat an anode is confronted by a cathode on each face, with a cellchamber there between. Examples of electrolysis cells that can comprisea plurality of anodes and cathodes are disclosed in U.S. Pat. No.5,534,120, issued to Ando et al. on Jul. 9, 1996, and U.S. Pat. No.4,062,754, issued to Eibl on Dec. 13, 1977, which are incorporatedherein by reference.

[0046] Generally, the electrolysis cell will have one or more inletopenings in fluid communication with each cell chamber, and one or moreoutlet openings in fluid communication with the chambers. The inletopening is also in fluid communication with the source of aqueous feedsolution, such that the aqueous feed solution can flow into the inlet,through the chamber, and from the outlet of the electrolysis cell. Theeffluent solution (the electrolyzed aqueous feed solution that exitsfrom the electrolysis cell) comprises an amount f mixed oxidant that wasconverted within the cell passage in response to the flow of electricalcurrent through the solution. The effluent solution can be used as asource of mixed oxidants, for example, for disinfecting articles, or fortreating other volumes of water or aqueous solutions. The effluent canitself be a treated solution, where the feed solution containsmicroorganisms or some other oxidizable source material that can beoxidized in situ by the mixed oxidant solution that is formed.

[0047] The present invention also provides a mixed oxidant generatingsystem, comprising:

[0048] a) a source of an aqueous feed solution comprising a halide salt;

[0049] b) a non-membrane electrolysis cell having a cell chamber, andcomprising an anode and a cathode, the cell chamber having a passageadjacent to the anode, and an inlet and an outlet in fluid communicationwith the cell chamber;

[0050] c) a means for passing the aqueous feed solution into the cellchamber, along the passage, and out of the outlet; and

[0051] d) an electric current supply to flow a current through theaqueous solution in the chamber, to convert a portion of the halide saltin the passage to mixed oxidants, and thereby form an aqueous effluentcomprising of mixed oxidants.

[0052]FIG. 1 and FIG. 2 show an embodiment of an electrolysis cell 10 ofthe present invention. The cell comprises an anode 21 electrode, and acathode 22 electrode. The electrodes are held a fixed distance away fromone another by a pair of opposed non-conductive electrode holders 30having electrode spacers 31 that space apart the confrontinglongitudinal edges of the anode and cathode to form a cell chamber 23having a chamber gap. The chamber 23 has a cell inlet 25 through whichthe aqueous feed solution can pass into of the cell, and an opposed celloutlet 26 from which the effluent can pass out of the electrolysis cell.The assembly of the anode and cathode, and the opposed plate holders areheld tightly together between a non-conductive anode cover 33 (shownpartially cut away) and cathode cover 34, by a retaining means (notshown) that can comprise non-conductive, water-proof adhesive, bolts, orother means, thereby restricting exposure of the two electrodes only tothe electrolysis solution that flows through the chamber 23. Anode lead27 and cathode lead 28 extend laterally and sealably through channelsmade in the electrode holders 30.

[0053]FIG. 2 shows cell chamber 23 and the passage 24 along the anode 21surface. The passage 24 is a portion of the cell chamber 23, though itis shown with a boundary 29 only to illustrate its adjacent to the anode21, and not to show the relative proportion or scale relative to thecell chamber.

[0054] Another embodiment of the electrolysis cell of the presentinvention is shown in FIG. 3. This electrolysis cell has an anode outlet35. The anode outlet removes a portion of the electrolyzed feed solutionflowing in the passage 24 adjacent the anode 21 as an anode effluent.The remainder of the cell effluent exits from the cell outlet 26, whichhereafter will also be referred to as the cathode effluent and thecathode outlet, respectively. Similar electrolysis cells that remove aportion of the electrolyzed solution flowing adjacent the anode throughan anode outlet are described in U.S. Pat. No. 5,316,740, issued toBaker et al. on May 31, 1994, U.S. Pat. No. 5,534,120 issued to Ando etal. on Jul. 9, 1996, and U.S. Pat. No. 5,858,201, issued to Otsuka etal. on Jan. 12, 1999. Particularly preferred is an electrolysis cell asshown in FIG. 3 of U.S. Pat. No. 4,761,208 that uses a physical barrier(element 16) positioned between the anode and the cathode adjacent theoutlet, whereby mixing of the solution adjacent the anode with thesolution adjacent the cathode can be minimized or eliminated prior toremoval through the anode outlet. Preferably, the cathode effluent,which will comprise a low level or no mixed oxidant product, is passedback to and mixed into the aqueous feed solution.

[0055] An electrode can generally have any shape that can effectivelyconduct electricity through the aqueous feed solution between itself andanother electrode, and can include, but is not limited to, a planarelectrode, an annular electrode, a spring-type electrode, and a porouselectrode. The anode and cathode electrodes can be shaped and positionedto provide a substantially uniform gap between a cathode and an anodeelectrode pair, as shown in FIG. 2. On the other hand, the anode and thecathode can have different shapes, different dimensions, and can bepositioned apart from one another non-uniformly. The importantrelationship between the anode and the cathode is for a sufficient flowof current through the anode at an appropriate voltage to promote theconversion of the halide salt to mixed oxidants within the cell passageadjacent the anode.

[0056] Planar electrodes, such as shown in FIG. 2, have a length alongthe flow path of the solution, and a width oriented transverse to theflow path. The aspect ratio of planar electrodes, defined by the ratioof the length to the width, is generally between 0.2 and 10, morepreferably between 0.1 and 6, and most preferably between 2 and 4.

[0057] The electrodes, both the anode and the cathode, are commonlymetallic, conductive materials, though non-metallic conductingmaterials, such as carbon, can also be used. The materials of the anodeand the cathode can be the same, but can advantageously be different. Tominimize corrosion, chemical resistant metals are preferably used.Examples of suitable electrodes are disclosed in U.S. Pat. No. 3,632,498and U.S. Pat. No. 3,771,385. Preferred anode metals are stainless steel,platinum, palladium, iridium, ruthenium, as well as iron, nickel andchromium, and alloys and metal oxides thereof. More preferred areelectrodes made of a metals such as titanium, tantalum, aluminum,zirconium, tungsten or alloys thereof, which are coated or layered witha Group VIII metal that is preferably selected from platinum, iridium,and ruthenium, and oxides and alloys thereof. One preferred anode ismade of titanium core and coated with, or layered with, ruthenium,ruthenium oxide, iridium, iridium oxide, and mixtures thereof, having athickness of at least 0.1 micron, preferably at least 0.3 micron.

[0058] For many applications, a metal foil having a thickness of about0.03 mm to about 0.3 mm can be used. Foil electrodes should be madestable in the cell so that they do not warp or flex in response to theflow of liquids through the passage that can interfere with properelectrolysis operation. The use of foil electrodes is particularlyadvantageous when the cost of the device must be minimized, or when thelifespan of the electrolysis device is expected or intended to be short,generally about one year or less. Foil electrodes can be made of any ofthe metals described above, and are preferably attached as a laminate toa less expensive electrically-conductive base metal, such as tantalum,stainless steel, and others.

[0059] A particularly preferred anode electrode of the presentinventions is a porous, or flow-through anode. The porous anode has alarge surface area and large pore volume sufficient to pass therethrough a large volume of aqueous feed solution. The plurality of poresand flow channels in the porous anode provide a greatly increasedsurface area providing a plurality of passages, through which theaqueous feed solution can pass. Porous media useful in the presentinvention are commercially available from Astro Met Inc. in Cincinnati,Ohio, Porvair Inc. in Henderson, N.C., or Mott Metallurgical inFarmington, Conn. Alternately U.S. Pat. Nos. 5,447,774 and 5,937,641give suitable examples of porous media processing. Preferably, theporous anode has a ratio of surface area (in square centimeters) tototal volume (in cubic centimeters) of more than about 5 cm⁻¹, morepreferably of more than about 10 cm⁻¹, even more preferably more thanabout 50 cm⁻¹, and most preferably of more than about 200 cm⁻¹.Preferably the porous anode has a porosity of at least about 10%, morepreferably of about 30% to about 98%, and most preferably of about 40%to about 70%. Preferably, the porous anode has a combination of highsurface area and electrical conductivity across the entire volume of theanode, to optimize the solution flow rate through the anode, and theconversion of chloride salt contained in the solution to the mixedoxidant product.

[0060] The flow path of the aqueous feed solution through the porousanode should be sufficient, in terms of the exposure time of thesolution to the surface of the anode, to convert the chloride salt tothe mixed oxidant. The flow path can be selected to pass the feedsolution in parallel with the flow of electricity through the anode (ineither the same direction or in the opposite direction to the flow ofelectricity), or in a cross direction with the flow of electricity. Theporous anode permits a larger portion of the aqueous feed solution topass through the passages adjacent to the anode surface, therebyincreasing the proportion of the halogen salt that can be converted tothe halogen containing mixed oxidant product.

[0061]FIG. 4 shows an electrolysis cell comprising a porous anode 21.The porous anode has a multiplicity of capillary-like flow passages 24through which the aqueous feed solution can pass adjacent to the anodesurfaces within the porous electrode. In the electrolysis cell of FIG.4, the aqueous feed solution flows in a parallel direction to the flowof electricity between the anode and the cathode.

[0062] Another embodiment of an electrolysis cell having a porous anodeis shown in FIG. 5. In this embodiment, the flow of aqueous feedsolution is in a cross direction to the flow of electricity between theanode and the cathode. Because the flow passages through the porousanode are generally small (less than 0.2 mm), the flow of a unit ofsolution through a porous anode will require substantially more pressurethat the same quantity flowing through an open cell chamber.Consequently, if aqueous feed solution is introduced into anelectrolysis cell having a porous anode and an open chamber, generallythe amount of solution flowing through the porous anode and across itssurfaces will be significantly diminished, since the solution will flowpreferentially through the open cell chamber.

[0063] To address the above problem where the aqueous feed solution canby-pass the porous anode, the cell chamber is preferably provided, asshown in FIG. 6, with a non-conducting, porous flow barrier 40, withinthe volume of the cell chamber 24 between the cathode 22 and the porousanode 21. The porous barrier 40 is non-conducting, to preventelectricity from short-circuiting between the anode and the cathode viathe chamber material. The porous barrier exerts a solution pressure dropas the aqueous feed solution flows through the cell chamber. The porousbarrier should not absorb or retain water, and should not react with theaqueous solution and chemical ingredients therein, including the mixedoxidant products. The porous barrier 40 can be made of a non-conductingmaterial selected from, but not limited to, plastics such aspolyethylene, polypropylene, and polyolefin, glass or other siliceousmaterial, and silicon. The porous barrier can comprise a plurality ofspheres, ovals, and other shaped objects of the same size or ofdifferent sizes, that can be packed loosely, or as a unified matrix ofarticles, into the chamber. FIG. 6 shows the porous barrier 40 as amatrix of spherical objects of varying diameters. The porous barrier 40can also be one or more baffles, which substantially restrict the flowof the solution through the cell chamber 24. As shown in FIG. 7, suchbaffles can comprise a series of vertical barriers having aperturestherein for restricting the flow of solution. The restricted flow ofaqueous feed solution through the non-conducting, porous barriersignificantly reduces the proportion of aqueous feed solution that canpass through cell chamber, thereby increasing the proportion of halidesalt that is converted in the passages 23 within the porous anode 21.

[0064] While the solution flowing through the porous anode and the cellchamber 24 containing the porous barrier 40 can mix and flow back andforth somewhat between each other, the effluents exiting from thedifferent areas of the outlet end 26 of the cell have substantiallydifferent solution compositions. The effluent 38 exiting the porousanode will have a significantly lower pH and higher production ofhalogen product than the effluent 39 exiting the cell chamber adjacentto the cathode. The effluent 38 exiting the porous anode can beseparated from the effluent 39 and removed from the cell by placing abarrier 37 as shown in FIG. 8.

[0065] Another embodiment of the present invention uses an electrolysiscell that has an open chamber. The open-chamber electrolysis cell isparticularly useful in the practice of the invention in reservoirs ofaqueous feed solution; including pools, bathtubs, spas, tanks, and otheropen bodies of water. The aqueous feed solution can flow into the celland to the anode from various directions. The halide salt in the aqueousfeed solution can be contained in the reservoir solution, or can bedelivered into the reservoir solution locally as a local source ofhalide salt, as herein before described. Examples of open-chamberelectrolysis cells include those described in U.S. Pat. No. 4,337,136(Dahlgren), U.S. Pat. No. 5,013,417 (Judd), U.S. Pat. No. 5,059,296(Sherman), and U.S. Pat. No. 5,085,753 (Sherman).

[0066] An alternative system for generating mixed oxidant comprises abatch container containing the aqueous feed solution. A re-circulatingpump circulates the feed solution from the container through anelectrolysis cell, and discharges the effluent back to the batchcontainer. In time, the concentration of the un-reacted chloride salt inthe solution will be reduced to essentially zero, whereby the chargedamount of sodium chloride in the aqueous feed solution will have beennearly completely converted to mixed oxidant product. In a slightlydifferent system, the electrolysis cell can be positioned within thebatch container, submerged within the aqueous solution comprising thesodium chloride. A pump or mixer within the container forces thesolution through the electrolysis cell, and re-circulates the solutionuntil the target conversion of sodium chloride to mixed oxidant isachieved.

[0067] The electrolysis cell can also comprise a batch-type cell thatelectrolyses a volume of the aqueous feed solution. The batch-type cellcomprises a batch chamber having a pair of electrodes. The batch chamberis filled with aqueous feed solution comprising the sodium chloridesalt, which is then electrolyzed to form a batch of effluent solutioncontaining mixed oxidant. The electrodes preferably comprise an outerannular anode and a concentric inner cathode. An example of a suitablebatch cell, for use with a sodium chloride salt supply in accordancewith the present invention, is disclosed in WO 00/71783-A1, publishedNov. 30, 2000, incorporated herein by reference.

Electrical Current Supply

[0068] An electrical current supply provides a flow of electricalcurrent between the electrodes and across the passage of aqueous feedsolution passing across the anode. For many applications, the preferredelectrical current supply is a rectifier of household (or industrial)current that converts common 100-230 volt AC current to DC current.

[0069] For applications involving portable or small, personal usesystems, a preferred electrical current supply is a battery or set ofbatteries, preferably selected from an alkaline, lithium, silver oxide,manganese oxide, or carbon zinc battery. The batteries can have anominal voltage potential of 1.5 volts, 3 volts, 4.5 volts, 6 volts, orany other voltage that meets the power requirements of the electrolysisdevice. Most preferred are common-type batteries such as “AA” size,“AAA” size, “C” size, and “D” size batteries having a voltage potentialof 1.5 V. Two or more batteries can be wired in series (to add theirvoltage potentials) or in parallel (to add their current capacities), orboth (to increase both the potential and the current). Re-chargeablebatteries and mechanical wound-spring devices can also be advantageouslyemployed.

[0070] Another alternative is a solar cell that can convert (and store)solar power into electrical power. Solar-powered photovoltaic panels canbe used advantageously when the power requirements of the electrolysiscell draws currents below 2000 milliamps across voltage potentialsbetween 1.5 and 9 volts. Many other known power sources may be used inpracticing this invention including, but not limited to, manual-crankgenerator systems and water pressure/flow turbine systems.

[0071] In one embodiment, the electrolysis cell can comprise a singlepair of electrodes having the anode connected to the positive lead andthe cathode connected to the negative lead of the battery or batteries.A series of two or more electrodes, or two or more cells (each a pair ofelectrodes) can be wired to the electrical current source. Arranging thecells in parallel, by connecting each cell anode to the positiveterminal(s) and each cell cathode to the negative terminal(s), providesthe same electrical potential (voltage) across each cell, and divides(evenly or unevenly) the total current between the two or more electrodepairs. Arranging two cells (for example) in series, by connecting thefirst cell anode to the positive terminal, the first cell cathode to thesecond cell anode, and the second cell cathode to the negative terminal,provides the same electrical current across each cell, and divides thetotal voltage potential (evenly or unevenly) between the two cells.

[0072] The electrical current supply can further comprise a circuit forperiodically reversing the output polarity of the battery or batteriesin order to maintain a high level of electrical efficacy over time. Thepolarity reversal minimizes or prevents the deposit of scale and theplating of any charged chemical species onto the electrode surfaces.Polarity reversal functions particularly well when using confrontinganode and cathode electrodes.

Electrolysis Effluent

[0073] In most applications, the microorganisms in the contaminatedsolution are killed as the solution, which already contains chloridesalt, is passed through the electrolysis device. In other applications,the discharged effluent containing the converted mixed oxidants isremoved from the electrolysis cell and is used, for example, as anaqueous disinfection solution. The effluent can be used as-made bydirect delivery to an oxidizable source that is oxidized by the mixedoxidants. The oxidizable source can be a second source of water or otheraqueous solution comprising microorganisms are destroyed when mixed orcontacted with the effluent solution. Microorganisms contained withinthe aqueous feed solution would also be destroyed.

Impurity Removal

[0074] Water impurities come in many forms. In some cases they are ofmicrobial nature and may be viral, bacterial, fungal, parasitic or otherbiological forms. The removal of some or all of these impurities may beassisted with a filter before or after the electrolytic cell. Ofparticular interest is the removal of 99.95% cyst organisms, such ascryptosporidium, which would be removed from the contaminated water ifthe effective filtration size of the filter is less than the size of thecysts (e.g. a filter capable of removing particulates greater than 3microns).

[0075] The impurities may also be non microbial. It may also be possibleto remove some of these impurities via a filter by size. In some cases,the contamination in water may also be of organic or inorganic nature.It would also be desirable for a filter to remove some or all of theorganic or inorganic contaminants. In other cases we may also want toconvert the form of the organic or inorganic species to one that is moreeasily removed via filtration. For example, arsenic (As) may exists inone of two oxidation levels (As(III) and As(V)). Generally, it isthought that As (III) is the more toxic form, but both oxidation levelshave negative health consequences. The oxidation state of As likely tobe found in water varies with the source. Surface water normally has ahigher percentage of As (V) than ground water owing to air oxidation.The structures of inorganic As(III) (arsenite) and As(V) (arsenate),plus their corresponding acid dissociation constants, are shown below.

Arsenate

[0076]

[0077] Note that at the pH of drinking water, As (V) will exist aseither a mono or divalent anion, whereas As(III) will exist as a neutralmolecule. This suggests that As(V), but not As(III), would easily beremoved from water by anion exchange resins. Therefore, if As(III) couldeasily be oxidized to As (V), ion exchange would represent an excellenttreatment option for the removal of As. With a typical strong base ionexchange resin the selectivity for the removal of anions likely to befound in water lies in the following order (easiest to hardest):sulfate>arsenate>nitrate>arsenite>chloride>bicarbonate.

[0078] There are some situations where the filter may consist, in partor in total, of an ion exchange resin as a pre-treatment to theelectrolytic solution entering the electrolytic cell. It would be ofparticular interest for the ion exchange resin to yield an effluent thatincreases the halide ion concentration in the electrolytic solutionprior to electrolysis, for example, by the use of an anion exchangeresin in the chloride form. The use of a cation exchange resin canminimize the concentration of scale forming ions such as calcium andmagnesium in the electrolysis cell, thus minimizing the need forcleaning the anode (s) and cathode (s).

EXAMPLES

[0079]FIG. 9 depicts a non-limiting exemplary embodiment of a flow cell100. Flow cell 100 may include an inlet 110 and an outlet 120. One mayuse a low powered (preferably, portable) electrolysis flow cell that canuse the current and voltage delivered by conventional householdbatteries. The electrolysis cells can come in various sizes, with anodeshaving a surface area of from about 0.1 cm² to about 60 cm². Oneparticularly preferred embodiment of the present invention comprises anelectrolysis cell with an anode having a surface area of from about 1cm² to about 20 cm², more preferably from about 3 cm² to about 10 cm².An electrically driven motorized pump can pump the solution to theelectrolysis cell via a flow cell configuration. Such pump units willtypically flow at rates from about 100 to about 300 cc/min. of solution.

[0080]FIG. 10 depicts a non-limiting exemplary embodiment of are-circulation cell 200, which includes cell 100. Recirculation cell 200may include an aqueous solution reservoir 204. Reservoir 204 may containan aqueous feed solution comprising a halogen salt. The solution leavingoutlet 120 may be introduced into reservoir 204 whereby the solutionwill mix with the aqueous feed solution resulting into a build-up of thedesired electrolyzed species. Once the both of these solutions aremixed, they are introduced into inlet 110. Both solutions may be movedabout by any currently known methods for moving like materials includingbut not limited to pump 206. Optionally, reservoir 204 may include aninlet 210 and an outlet 220 to allow the introduction of additionalaqueous feed solution and the exiting of electrolyzed solution so thatit may be utilized.

[0081]FIG. 11 depicts a non-limiting exemplary embodiment of a flow cell100. Flow cell 100 may include a prefilter device 300. Prefilter device300 may be used to filter out a variety of undesired componentsincluding, but not limited to, sediments, particulates, insolublematerials, large organisms (e.g. cyst) from an aqueous feed solution.Filter mechanism 300 may be constructed of a variety of materials toachieved the desired benefits including, but not limited to, granulatedactivated carbon filter, granulated activated carbon block, activatedcarbon fibers, diatomaceous earth glass fibers, filter paper, ionexchange resins, size exclusion materials, charged-modified materials(an example illustrated in WO0107090A1 and thus is herein incorporatedby reference), zeolites, activated alumina, silica gel, calcium sulfate,fuller's earth, and activated bauxite. It may be further desirable toremove 99.95% of particulates having a size of at least 3 microns orgreater from the electrolytic solution for applications involvingdrinking water in order to meet ANSI/NSF standard 53.

[0082]FIG. 12 depicts a non-limiting exemplary embodiment of are-circulation cell 200 similar to that shown in FIG. 10 but alsoincluding a filter mechanism similar to that shown in FIG. 11.

[0083]FIG. 13 depicts a non-limiting exemplary embodiment of a flow cell100. Flow cell 100 may include an on-off sensor 400. On-off sensor 400may be used to detect the presence of an incoming aqueous feed solutionand in response may turn on the power supply (not shown), which is usedas the electrical power needed for electrolyzing the aqueous solution.In a similar fashion, on-off sensor may detect the absence of anincoming aqueous feed solution and in response may turn off the powersupply (not shown).

[0084]FIG. 14 depicts a non-limiting exemplary embodiment of are-circulation cell 200 similar to that shown in FIG. 10 but alsoincluding an on-off sensor similar to that shown in FIG. 13.

[0085]FIG. 15 depicts a non-limiting exemplary embodiment of a blockdiagram of a flow cell having an ion exchange resin 500. This ionexchange resin may serve two purposes. First, it may serve as a watersoftener to reduce the total hardness of the water passing through cell100. Secondly, it may serve as a halide anion exchanger whereby anionexchange resin would be used to exchange anion halide ions fornon-halide ions naturally present in the water to increase theefficiency of the system. An example of a halogen anion that could beexchanged readily for most anions in water is chloride.

[0086] A water softener is designed to reduce the total hardness ofwater. Total hardness may be measured chemically by the amount ofcalcium bicarbonate and magnesium bicarbonate content of the water. Awater softener is a specific type of ion exchange resin waterconditioner. Typically, cation exchange resin is used to exchangecalcium and magnesium cation in the water for other, normallymonovalent, cations. The most common exchange ions are sodium orhydrogen ions. Most water softening systems also include a means forregenerating the cation exchange resin bed. The most common method forregeneration of the resin is a brine solution flush. Sodium chloridesalt is normally used for this purpose.

[0087]FIG. 16 depicts a non-limiting exemplary embodiment of are-circulation cell 200 similar to that shown in FIG. 10 but alsoincluding an ion exchange resin 500 similar to that shown in FIG. 15.

Example 1 Flow Cell and Naturally Present Salt in Water

[0088] An electrolysis cell of the general design shown in FIG. 9 wasused to treat de-chlorinated tap water. The electrolysis cell had a pairof confronting electrodes having a passage gap of about 0.46 mm. Theanode was made of ES300—titanium, coated with ruthenium oxide andiridium oxide. The cathode was made of 201 stainless steel. Thedimensions of the planar electrodes were 73.0 mm long by 25.4 mm wide.The surface area of the electrode was calculated by multiplying thelength of the electrode by the width of the electrode (e.g. 7.30 cm×2.54cm=18.54 cm2). The de-chlorinated water was prepared by passing tapwater through a PuR faucet mount filter (carbon block filter) andremoving the chlorine from the water. The electric conductivity of thetap water used is 150 μS/cm. The amount of chloride ions measured in thetap water was 78 ppm. Ten liters of de-chlorinated water was collected.A peristaltic pump metered the solution from the glass container throughthe electrolysis cell at a flow rate of 300 ml/minute. A voltagepotential of 4.5 volts was provided across the electrolysis cell at acurrent of 0.43 amps via a power supply (Tenma Laboratory, Model72-630A). The resulting power was calculated by multiplying the voltageby the current (e.g. 4.5 V×0.44 A=1.98 W). The effluent solution waswithdrawn from the electrolysis cell and analyzed. The effluentcontained a total of 2.90 ppm concentration of mixed oxidants asmeasured via the DPD Hach method for free chlorine. The productivityindex achieved was 439 as measured by the efficiency calculationdescribed in equation I (η=(CMO*Q)/(I*V)). Various other test conditionsare listed in table A. TABLE A Electrode Flow Electrode Spacing RateVoltage Current Surface Oxidant Conc'n Productivity (mm) (ml/min) (V)(A) Power (W) Area (cm2) (ppm) Index 0.46 100 4.5 0.65 2.93 18.5 12.56429 0.46 500 4.5 0.44 1.98 18.5 1.42 359 0.46 1000 4.5 0.40 1.80 18.50.54 300 0.46 100 6.0 1.14 6.84 18.5 20.90 306 0.46 500 6.0 0.87 5.2218.5 3.03 290 0.46 1000 6.0 0.73 4.38 18.5 1.13 258 0.23 100 4.5 0.321.44 9.0 4.60 319 0.23 500 4.5 0.23 1.04 9.0 0.72 346 0.23 1000 4.5 0.220.99 9.0 0.33 333 0.23 100 6.0 0.67 4.02 9.0 7.88 196 0.23 500 6.0 0.452.70 9.0 1.20 222 0.23 1000 6.0 0.41 2.46 9.0 0.59 240 0.46 100 4.5 0.251.13 9.0 3.53 312 0.46 500 4.5 0.20 0.90 9.0 0.44 244 0.46 1000 4.5 0.180.81 9.0 0.12 148 0.46 100 6.0 0.42 2.52 9.0 6.18 245 0.46 500 6.0 0.302.34 9.0 0.83 177 0.46 1000 6.0 0.35 2.10 9.0 0.26 124 0.23 100 4.5 0.190.86 4.5 2.08 242 0.23 500 4.5 0.13 0.59 4.5 0.23 195 0.23 1000 4.5 0.120.54 4.5 0.05 93 0.23 100 6.0 0.41 2.46 4.5 3.80 154 0.23 500 6.0 0.251.50 4.5 0.44 147 0.23 1000 6.0 0.22 1.32 4.5 0.14 106 0.46 100 4.5 0.070.32 4.5 0.99 309 0.46 500 4.5 0.06 0.27 4.5 0.13 241 0.46 1000 4.5 0.060.27 4.5 0.04 148 0.46 100 6.0 0.14 0.84 4.5 1.80 214 0.46 500 6.0 0.110.66 4.5 0.28 212 0.46 1000 6.0 0.11 0.66 4.5 0.10 152

Example 2 Flow Cell and Water with Salt Added

[0089] The electrolysis cell of Example 1 was operated using an aqueousfeed solution consisting of a prepared salt solution. Sodium chloridesalt was added to de-ionized water. For this test, 500 mg of technicalgrade sodium chloride (Aldrich Chemical Company, Inc, Milwaukee, Wis.53233) was added and mixed with a stirring bar until dissolved, forminga 50 ppm chloride from a sodium chloride salt solution. The aqueous feedsolution was retained in a 10-liter glass container. A peristaltic pumpmetered the solution from the glass container through the electrolysiscell at a flow rate of 300 ml/minute. A voltage potential of 4.5 voltswas provided across the electrolysis cell at a current of 0.22 amps. Theeffluent solution was withdrawn from the electrolysis cell and analyzed.The effluent contained 2.13 ppm oxidants. The calculated productivityindex was 645.

Example 3 Flow Cell with AA Batteries

[0090] The electrolysis cell of Example 1 was operated in a similar wayas described in example 1 but the power supply was replaced with 3 AAbatteries (Duracell). A peristaltic pump metered the de-chlorinatedwater from the glass container through the electrolysis cell at a flowrate of 300 ml/minute. From the 3 AA batteries, a voltage potential of4.1 volts was provided across the electrolysis cell and a current of0.34 amps was measured. The effluent solution was withdrawn from theelectrolysis cell and analyzed. The effluent contained 1.96 ppm oxidant.The calculated productivity index was 427.

Example 4 Re-circulating Cell with Naturally Present Salt in Water

[0091] The electrolysis cell of FIG. 10 was operated under the sameoperating conditions as that listed in example 1. The free oxidantconcentration of the 10 liter of water increases over time. Results areshown in Table B below. TABLE B Electrode Electrode Spacing Time VoltageCurrent Power Surface Oxidant Conc'n (mm) (min) (V) (A) (W) Area (cm2)(ppm) 0.46 0 0 0 0 18.5 0 0.46 1 4.5 0.43 1.94 18.5 0.06 0.46 3 4.5 0.452.03 18.5 0.23 0.46 5 4.5 0.44 1.98 18.5 0.41 0.46 10 4.5 0.45 2.03 18.50.83 0.46 20 4.5 0.45 2.03 18.5 1.55 0.46 30 4.5 0.45 2.03 18.5 2.31

[0092] The present invention may be appreciated in a multitude ofapplications including, but not limited to, faucet-mounted filters,counter-top water purification devices, under-sink water purificationdevices, camping/backpack water purification devices, travel waterpurification devices, refrigerator water purification devices,pitcher-type gravity flow water purification devices, bathing waterpurification devices, and spa-type water purification devices.

[0093] The various advantages of the present invention will becomeapparent to those skilled in the art after a study of the foregoingspecification and following claims.

What is claimed is:
 1. An apparatus for electrolyzing an electrolyticsolution, said apparatus comprising: (a) a non-barrier electrolytic cellcomprising: (i.) an anode; (ii.) a cathode, said anode and said cathodedefining a passage formed therebetween; (iii.) an inlet portcommunicating with said passage, said inlet port used to receive a flowof electrolytic solution; and (iv.) an outlet port communicating withsaid passage, said outlet port providing an exit for the flow ofelectrolytic solution having been electrolyzed; and (b) a current supplyfor providing an electrical current from said anode to said cathode,wherein said current supply delivers less than about 5 watts of power,wherein the electrical current electrolyzes the flow of electrolyticsolution.
 2. The apparatus according to claim 1 wherein said apparatusfurther comprising a body, said body providing containment for saidelectrolytic cell and said current supply.
 3. The apparatus according toclaim 1 wherein said apparatus further comprising a fluid movementmechanism for moving electrolytic solution into said inlet port and outof said outlet port.
 4. The apparatus according to claim 3 wherein saidfluid movement mechanism recirculates electrolytic solution that hasexited said outlet port back into said inlet port in order to repeat theelectrolyzing of the electrolytic solution.
 5. The apparatus accordingto claim 1 wherein said apparatus further comprising a filter forremoval of impurities.
 6. The apparatus according to claim 5 whereinsaid filter is positioned before said electrolytic cell.
 7. Theapparatus according to claim 5 wherein said filter is positioned aftersaid electrolytic cell.
 8. The apparatus according to claim 5 whereinsaid filter is adapted to remove 99.95% of particulates having a size ofat least 3 microns or greater from the electrolytic solution.
 9. Theapparatus according to claim 5 wherein said filter removes organicspecies.
 10. The apparatus according to claim 9 wherein said filter ispositioned after said electrolytic cell and said electrolytic cellconverts the organic species to a form that is removable by said filter.11. The apparatus according to claim 5 wherein said filter removesinorganic species.
 12. The apparatus according to claim 11 wherein saidfilter is positioned after said electrolytic cell and said electrolyticcell converts the oxidation state of inorganic species to a state thatis removable by said filter.
 13. The apparatus according to claim 11wherein said filter is adapted to remove arsenic.
 14. The apparatusaccording to claim 11 wherein said filter is positioned after saidelectrolytic cell and said electrolytic cell converts the oxidationstate of arsenic to a state that is removable by said filter.
 15. Theapparatus according to claim 11 wherein said filter is positioned aftersaid electrolytic cell.
 16. The apparatus according to claim 5 whereinsaid filter is constructed in part or in total of a resin.
 17. Theapparatus according to claim 5 wherein said filter is constructed inpart or in total of carbon.
 18. The apparatus according to claim 1wherein said apparatus further comprising an ion exchange resin as apre-treatment to the electrolytic solution prior to electrolysis. 19.The apparatus according to claim 18 wherein said ion exchange resin isadapted to increase the halogen-containing ion concentration of theelectrolytic solution.
 20. The apparatus according to claim 18 whereinsaid ion exchange resin is adapted to decrease the concentration ofscale-forming ions from the electrolytic solution.
 21. The apparatusaccording to claim 18 wherein said ion exchange resin is a watersoftener.
 22. The apparatus according to claim 1 wherein said apparatusfurther comprising a water-presence sensor capable of triggering thestart of the electrolysis process in the presence of water and alsocapable of triggering the stop of the electrolysis process in theabsence of water.
 23. The apparatus according to claim 22 wherein saidwater-presence sensor is a field effect transistor.
 24. The apparatusaccording to claim 1 wherein said current supply is selected from agroup consisting of battery, ac-dc converter, solar cell, manual crankgenerator system, water pressure/turbine energy system and combinationsthereof.
 25. The apparatus according to claim 1 wherein said anode is afoil electrode.
 26. The apparatus according to claim 1 wherein saidanode comprises a Group VIII metal.
 27. The apparatus according to claim1 wherein the anode is a porous anode.
 28. The apparatus according toclaim 1 wherein the porous anode is a porous metallic anode.
 29. Theapparatus according to claim 1 wherein said apparatus is adapted to beused as one or more of the following applications: faucet-mountedfilters, counter-top water purification devices, under-sink waterpurification devices, camping/backpack water purification devices,travel water purification devices, refrigerator water purificationdevices, pitcher-type gravity flow water purification devices, bathingwater purification devices, and spa-type water purification devices. 30.The apparatus according to claim 1 wherein said apparatus is adapted toremove impurities.
 31. The apparatus according to claim 1 wherein saidapparatus is adapted to kill microorganisms.
 32. An apparatus forelectrolyzing an electrolytic solution, said apparatus comprising: (a) anon-barrier electrolytic cell comprising: (i.) an anode, wherein asurface area of said anode is less than about 30 cm2; (ii.) a cathode,said anode and said cathode defining a passage formed therebetween;(iii.) an inlet port communicating with said passage, said inlet portused to receive a flow of electrolytic solution; and (iv.) an outletport communicating with said passage, said outlet port providing an exitfor the flow of electrolytic solution having been electrolyzed; and (b)a current supply for providing an electrical current from said anode tosaid cathode, wherein said current supply delivers less than about 5watts of power, wherein the electrical current electrolyzes the flow ofelectrolytic solution.
 33. The apparatus according to claim 32 whereinsaid apparatus further comprising a body, said body providingcontainment for said electrolytic cell and said current supply.
 34. Theapparatus according to claim 32 wherein said apparatus furthercomprising a fluid movement mechanism for moving electrolytic solutioninto said inlet port and out of said outlet port.
 35. The apparatusaccording to claim 34 wherein said fluid movement mechanism recirculateselectrolytic solution that has exited said outlet port back into saidinlet port in order to repeat the electrolyzing of the electrolyticsolution.
 36. The apparatus according to claim 32 wherein said apparatusfurther comprising a filter for removal of impurities.
 37. The apparatusaccording to claim 36 wherein said filter is positioned before saidelectrolytic cell.
 38. The apparatus according to claim 36 wherein saidfilter is positioned after said electrolytic cell.
 39. The apparatusaccording to claim 36 wherein said filter is adapted to remove 99.95% ofparticulates having a size of at least 3 microns or greater from theelectrolytic solution.
 40. The apparatus according to claim 36 whereinsaid filter removes organic species.
 41. The apparatus according toclaim 40 wherein said filter is positioned after said electrolytic celland said electrolytic cell converts the organic species to a form thatis removable by said filter.
 42. The apparatus according to claim 36wherein said filter removes inorganic species.
 43. The apparatusaccording to claim 42 wherein said filter is positioned after saidelectrolytic cell and said electrolytic cell converts the oxidationstate of inorganic species to a state that is removable by said filter.44. The apparatus according to claim 42 wherein said filter is adaptedto remove arsenic.
 45. The apparatus according to claim 42 wherein saidfilter is positioned after said electrolytic cell and said electrolyticcell converts the oxidation state of arsenic to a state that isremovable by said filter.
 46. The apparatus according to claim 42wherein said filter is positioned after said electrolytic cell.
 47. Theapparatus according to claim 36 wherein said filter is constructed inpart or in total of a resin.
 48. The apparatus according to claim 36wherein said filter is constructed in part or in total of carbon. 49.The apparatus according to claim 32 wherein said apparatus furthercomprising an ion exchange resin as a pre-treatment to the electrolyticsolution prior to electrolysis.
 50. The apparatus according to claim 49wherein said ion exchange resin is adapted to increase thehalogen-containing ion concentration of the electrolytic solution. 51.The apparatus according to claim 49 wherein said ion exchange resin isadapted to decrease the concentration of scale-forming ions from theelectrolytic solution.
 52. The apparatus according to claim 49 whereinsaid ion exchange resin is a water softener.
 53. The apparatus accordingto claim 32 wherein said apparatus further comprising a water-presencesensor capable of triggering the start of the electrolysis process inthe presence of water and also capable of triggering the stop of theelectrolysis process in the absence of water.
 54. The apparatusaccording to claim 53 wherein said water-presence sensor is a fieldeffect transistor.
 55. The apparatus according to claim 32 wherein saidcurrent supply is selected from a group consisting of battery, ac-dcconverter, solar cell, manual crank generator system, waterpressure/turbine energy system and combinations thereof.
 56. Theapparatus according to claim 32 wherein said anode is a foil electrode.57. The apparatus according to claim 32 wherein said anode comprises aGroup VIII metal.
 58. The apparatus according to claim 32 wherein theanode is a porous anode.
 59. The apparatus according to claim 32 whereinthe porous anode is a porous metallic anode.
 60. The apparatus accordingto claim 32 wherein said apparatus is adapted to be used as one or moreof the following applications: faucet-mounted filters, counter-top waterpurification devices, under-sink water purification devices,camping/backpack water purification devices, travel water purificationdevices, refrigerator water purification devices, pitcher-type gravityflow water purification devices, bathing water purification devices, andspa-type water purification devices.
 61. The apparatus according toclaim 32 wherein said apparatus is adapted to remove impurities.
 62. Theapparatus according to claim 32 wherein said apparatus is adapted tokill microorganisms.
 63. An apparatus for electrolyzing an electrolyticsolution, said apparatus comprising: (a) a non-barrier electrolytic cellcomprising: (i.) an anode; (ii.) a cathode, said anode and said cathodedefining a passage formed therebetween, said passage having a distancebetween said anode and said cathode of less than about 0.6 mm; (iii.) aninlet port communicating with said passage, said inlet port used toreceive a flow of electrolytic solution; and (iv.) an outlet portcommunicating with said passage, said outlet port providing an exit forthe flow of electrolytic solution having been electrolyzed; and (b) acurrent supply for providing an electrical current from said anode tosaid cathode, wherein said current supply delivers less than about 5watts of power, wherein the electrical current electrolyzes the flow ofelectrolytic solution.
 64. The apparatus according to claim 63 whereinsaid apparatus further comprising a body, said body providingcontainment for said electrolytic cell and said current supply.
 65. Theapparatus according to claim 63 wherein said apparatus furthercomprising a fluid movement mechanism for moving electrolytic solutioninto said inlet port and out of said outlet port.
 66. The apparatusaccording to claim 65 wherein said fluid movement mechanismre-circulates electrolytic solution that has exited said outlet portback into said inlet port in order to repeat the electrolyzing of theelectrolytic solution.
 67. The apparatus according to claim 63 whereinsaid apparatus further comprising a filter for removal of impurities.68. The apparatus according to claim 67 wherein said filter ispositioned before said electrolytic cell.
 69. The apparatus according toclaim 67 wherein said filter is positioned after said electrolytic cell.70. The apparatus according to claim 67 wherein said filter is adaptedto remove 99.95% of particulates having a size of at least 3 microns orgreater from the electrolytic solution.
 71. The apparatus according toclaim 67 wherein said filter removes organic species.
 72. The apparatusaccording to claim 71 wherein said filter is positioned after saidelectrolytic cell and said electrolytic cell converts the organicspecies to a form that is removable by said filter.
 73. The apparatusaccording to claim 67 wherein said filter removes inorganic species. 74.The apparatus according to claim 73 wherein said filter is positionedafter said electrolytic cell and said electrolytic cell converts theoxidation state of inorganic species to a state that is removable bysaid filter.
 75. The apparatus according to claim 73 wherein said filteris adapted to remove arsenic.
 76. The apparatus according to claim 73wherein said filter is positioned after said electrolytic cell and saidelectrolytic cell converts the oxidation state of arsenic to a statethat is removable by said filter.
 77. The apparatus according to claim73 wherein said filter is positioned after said electrolytic cell. 78.The apparatus according to claim 67 wherein said filter is constructedin part or in total of a resin.
 79. The apparatus according to claim 67wherein said filter is constructed in part or in total of carbon. 80.The apparatus according to claim 63 wherein said apparatus furthercomprising an ion exchange resin as a pre-treatment to the electrolyticsolution prior to electrolysis.
 81. The apparatus according to claim 80wherein said ion exchange resin is adapted to increase thehalogen-containing ion concentration of the electrolytic solution. 82.The apparatus according to claim 80 wherein said ion exchange resin isadapted to decrease the concentration of scale-forming ions from theelectrolytic solution.
 83. The apparatus according to claim 80 whereinsaid ion exchange resin is a water softener.
 84. The apparatus accordingto claim 63 wherein said apparatus further comprising a water-presencesensor capable of triggering the start of the electrolysis process inthe presence of water and also capable of triggering the stop of theelectrolysis process in the absence of water.
 85. The apparatusaccording to claim 84 wherein said water-presence sensor is a fieldeffect transistor.
 86. The apparatus according to claim 63 wherein saidcurrent supply is selected from a group consisting of battery, ac-dcconverter, solar cell, manual crank generator system, waterpressure/turbine energy system and combinations thereof.
 87. Theapparatus according to claim 63 wherein said anode is a foil electrode.88. The apparatus according to claim 63 wherein said anode comprises aGroup VIII metal.
 89. The apparatus according to claim 63 wherein theanode is a porous anode.
 90. The apparatus according to claim 63 whereinthe porous anode is a porous metallic anode.
 91. The apparatus accordingto claim 63 wherein said apparatus is adapted to be used as one or moreof the following applications: faucet-mounted filters, counter-top waterpurification devices, under-sink water purification devices,camping/backpack water purification devices, travel water purificationdevices, refrigerator water purification devices, pitcher-type gravityflow water purification devices, bathing water purification devices, andspa-type water purification devices.
 92. The apparatus according toclaim 63 wherein said apparatus is adapted to remove impurities.
 93. Theapparatus according to claim 63 wherein said apparatus is adapted tokill microorganisms.